CN1075396C - Reactor, process and plant for manufacturing ammonium salts - Google Patents
Reactor, process and plant for manufacturing ammonium salts Download PDFInfo
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- CN1075396C CN1075396C CN97102296A CN97102296A CN1075396C CN 1075396 C CN1075396 C CN 1075396C CN 97102296 A CN97102296 A CN 97102296A CN 97102296 A CN97102296 A CN 97102296A CN 1075396 C CN1075396 C CN 1075396C
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01C—AMMONIA; CYANOGEN; COMPOUNDS THEREOF
- C01C1/00—Ammonia; Compounds thereof
- C01C1/28—Methods of preparing ammonium salts in general
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J19/24—Stationary reactors without moving elements inside
- B01J19/2415—Tubular reactors
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J19/26—Nozzle-type reactors, i.e. the distribution of the initial reactants within the reactor is effected by their introduction or injection through nozzles
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01C—AMMONIA; CYANOGEN; COMPOUNDS THEREOF
- C01C1/00—Ammonia; Compounds thereof
- C01C1/18—Nitrates of ammonium
- C01C1/185—Preparation
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J2219/00049—Controlling or regulating processes
- B01J2219/00051—Controlling the temperature
- B01J2219/00159—Controlling the temperature controlling multiple zones along the direction of flow, e.g. pre-heating and after-cooling
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J2219/00049—Controlling or regulating processes
- B01J2219/00162—Controlling or regulating processes controlling the pressure
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J2219/00049—Controlling or regulating processes
- B01J2219/00164—Controlling or regulating processes controlling the flow
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J2219/00049—Controlling or regulating processes
- B01J2219/00177—Controlling or regulating processes controlling the pH
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J2219/00049—Controlling or regulating processes
- B01J2219/00182—Controlling or regulating processes controlling the level of reactants in the reactor vessel
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Inorganic Chemistry (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Physical Or Chemical Processes And Apparatus (AREA)
- Fertilizers (AREA)
- Treating Waste Gases (AREA)
Abstract
A process for manufacturing ammonium salts using a reactor which includes a first tubular reaction chamber (110) having at least one acid feed (112) and at least on ammonia feed (111) which are arranged in a first up-stream part of the reactor. At least one second ammonia feed is introduced into a second part (R2) of the reactor which is arranged as an extension of the first and which includes, in a flow direction, a convergent (122) segment, a cylindrical tube (121) and a divergent segment (123). The second ammonia feed (124) communicates with the second part in the vicinity of the convergent segment and the processes is controlled to obtain basic vapors at an outlet of the reactor.
Description
The present invention relates in particular as the manufacturing of the ammonium salt of fertilizer.
Specifically, the method for using tubular reactor manufacturing ammonium salt is disclosed in many documents (United States Patent (USP) the 2nd, 568, No. 901, the 2nd, 755, No. 176 and the 2nd, 902, No. 342).According to these methods, two kinds of reagents (bronsted lowry acids and bases bronsted lowry) close stoichiometrical ratio with basic symbols and send into a tubular reaction chamber.This reaction chamber itself is extending a diameter significantly less than the pipe of reaction chamber diameter, continues neutralization reaction therein.One in two kinds of reagent transfer limes can axially feed reaction chamber, and another then tangentially feeds.Because equipment can produce the member of turbulent flow, for example Venturi tube, traverse baffle etc. have promoted its mixing.
Total length with the pipe extension chamber reaction chamber generally very big (often greater than the diameter of pipe 50 times) is so that as far as possible fully carry out neutralization reaction.
Have found that, in this reactor and method, make unneutralized nitric acid droplet have corrodibility from the high temperature (in the reaction of ammonia and nitric acid, this temperature can between 150 ℃ and 220 ℃) of the thermopositive reaction of alkali and acid.This can destroy reactor rapidly, promptly need change after about 6 to 12 months.For example using titanium to substitute stainless steel can improve work-ing life, but this can make the cost of reactor too high.
People also find in above-mentioned existing method, although used stoichiometric calculation ratio and total reactor length longer, reaction carry out and not exclusively, ammonia is still stayed reactor outlet from the nitrate separated steam.
Purpose of the present invention mainly is first problem in the above-mentioned two problems, that is, reduce or as eliminate corrosion to reactor if possible.
The present invention also aims to reduce the loss of ammonia, thereby improve the output of neutralization reaction.
For this purpose, primary theme of the present invention is a kind of reactor of making ammonium salt, this reactor comprises a tubular reaction chamber, at least one sour transfer lime, at least one ammonia transfer lime, the first part that they split at reactor is in the upstream portion, it is characterized in that: reactor also comprises a second section of arranging in the extension of first part, it comprises on flow direction: a contraction section, a round shape part and an expansion, be provided with at least one the second ammonia transfer limes, it feeds described reactor near the upstream extremity of described second section.
According to further feature of the present invention:
The second section of-reactor comprises a unique pipe;
-second section comprises pipe in an outer tube and, forms a vacuum doughunt therebetween, is connected with the internal capacity of interior pipe in its downstream end at least;
-part at its upstream, interior pipe comprises the passage that at least one is communicated with vacuum doughunt.
Another theme of the present invention is a kind of method of making ammonium salt, the reagent that comprises at least a acid and ammonia in this method is introduced near the upstream extremity of a tubular reactor, then, salt in expansion chamber solution and the vapor removal that leaves reactor, it is characterized in that: 80% to 99% of reagent total flux is introduced in the upstream portion of reactor with stoichiometric ratio substantially, the upstream extremity of the reactor second section of the ammonia of rest part in the extension that is arranged in first part is introduced reactor, therefore, separated steam has the pH value of alkalescence in expansion chamber, the alkaline steam that leaves expansion chamber is contacted with the rest part of acid, thereby in an additional step, finish neutralization reaction.
Further feature according to the method described above:
-ammonia the stream of introducing the reactor second section is controlled, so that partly obtain the excess ammonia that needs in reactor downstream, and the after separating in expansion chamber obtains the alkaline pH value more preferably greater than 9;
The described additional step of-end neutralization reaction realizes that by using washing soln and alkaline steam to neutralize described washing soln is to be made of the ammonium salt of recirculation and sour mixture.
Another theme of the present invention is an equipment of making ammonium salt, and it is used to implement above-mentioned method, particularly comprises according to reactor of the present invention.
More particularly, this equipment comprises a tubular reactor, and at least one ammonia transfer lime and at least one feeds reactor first part, promptly, the sour transfer lime of upstream portion, described reactor passes to an expansion chamber, in expansion chamber, salt in the solution separates with vapor phase, it is characterized in that: described reactor is produced according to the present invention, is provided with an additional class, in additional class, steam from expansion chamber contacts with the acid of rest part, so that realize neutralization reaction completely.
Contrast the following drawings now, describe the present invention in detail with way of example:
Fig. 1 to Fig. 4 is the sectional side elevation according to four kinds of tubular reactors of the present invention;
Fig. 5 is the sectional view along 5-5 line among Fig. 4;
Fig. 6 is a synoptic diagram of implementing the equipment of manufacturing ammonium salt of the present invention.
Fig. 1 represents to comprise three part R
1, R
2, R
3Tubular reactor R.First part, that is, and upstream portion R
1Constitute a reaction chamber 110, on the one hand, an axial ammonia transfer lime 111, on the other hand, one radially or preferably tangential sour transfer lime 112 send into reaction chamber, but above-mentioned two transfer limes can be put upside down or change.
Second section comprises the pipe 121 of a diameter less than the caliber of delimit chamber 110, and its upstream portion is extended by a contraction section 122, and its downstream part is extended by an expansion 123.Ammonia transfer lime 124 preferably tangentially sends into one near contraction section 122 upstream arrangement, and diameter equals the short cylinder shape pipe portion of the caliber of defined reaction chamber 110 substantially.For the ease of making, ammonia transfer lime 124 can be arranged in reactor part R
1And R
2Between the upstream that connects of flange.In this case, axial location flange 116,126 and pipe 124 is put upside down substantially in Fig. 1.
Reactor also is provided with the 3rd pipe 130, and it is fixed on part R
2Downstream end, its diameter approaches or is slightly smaller than pipe 110 diameter, and its length is 10 to 50 times of its diameter.But, preferably utilize improvement of the present invention, make part R
3Length short as much as possible, make its be shorter than well known device the length that must have.
In embodiment illustrated in fig. 2, use identical numeral to add 100 with similar part among Fig. 1.Second section comprises that a diameter equals the outer tube and the less interior pipe 221 of a diameter of part 210 diameters substantially, and interior pipe 221 part at its upstream has a contraction section 222, and an expansion 223 is arranged in its downstream part.Should fix by flange 225 at its upstream end by interior pipe, flange 225 is clamped between two flanges 216,226, and 216,226 of flanges are separately fixed on part 210 and the outer tube 220, thereby pipe is in the state of overhanging in making.
Form a ringwise substantially chamber 227 between outer tube and interior pipe, the ammonia transfer lime feeds near this chamber upstream extremity.
Reactor shown in Figure 3 and structure of reactor shown in Figure 2 are very similar, and still, regional at its upstream, pipe 321 comprises the hole 328 of a plurality of bunchiness in the round shape, and this pipe is communicated with vacuum doughunt 327.These holes are positioned near the ammonia source that is made of tangential pipe 324.
In addition, interior pipe upstream extremity is directed in outer tube by at least three separators 329.
In modification shown in Figure 4, reactor R comprises three part R
1, R
2, R
3With the same in the previous examples, upstream portion comprises a pipe portion 410, and axial and tangential reagent transfer lime 411 and 412 feeds wherein.
The second section R of reactor
2Comprise that a diameter equals to manage the outer tube 420 of 410 diameter substantially.
This outer tube comprises a contraction section 440 that constitutes truncated cone shape pipe portion, be fixed between pipe portion 410 and 420 by a flange 441, also comprise one by flange 426 near the interior pipe that is fixed on its downstream end between pipe portion 420 and the pipe portion 430, pipe portion 430 constitutes the third part R of reactors
3
Should comprise that 421, one in a cylindrical tube portion was positioned at its upstream extremity by interior pipe, inlet diameter is greater than the expansion 422 of the exit diameter of contraction section 440, and an expansion 423 that is positioned at its downstream end.Interior pipe preferably includes strengthening rib 421a that extends and the separator 429 that is used to it is directed to respect to outer tube on its total length.
The downstream end of interior pipe comprises its opening 428 inner and vacuum doughunt 427 (Figure 4 and 5) of a plurality of connections.
In this illustrated example, the third part R of reactor
3Comprise that a middle interconnecting piece divides 431 and one pipe 432, its diameter is slightly smaller than pipe 420, and its length be in 10 to 50 times the scope of its diameter, still is preferably in the lower region of this scope, perhaps even be lower than this scope.
Now consult Fig. 6 and describe the equipment of making ammonium salt such as ammonium nitrate, be equipped with in this equipment according to reactor R of the present invention, for example it can be the form of above-mentioned a certain embodiment.
Except reactor R, aforesaid device also comprises expansion chamber D and treating column T.
Expansion chamber comprises a jar 500, and the end of reactor R preferably tangentially feeds in the jar 500, so that make the ammonium nitrate solution that flows downward and the mobile vapor removal that makes progress effectively, and emits by managing 501.Preferably include a droplet separation device at an upper portion thereof, this device is textile mat, bubble plate or packing form, or other any equality unit, and it can retain any droplet that is carried by steam.Be conical in its underpart, be connected in pipe 505 so that discharge ammonium nitrate solution.
Treating column or washing tower T can comprise following part from bottom to up:
-one flow container 510;
-one injection is by managing 501 devices 511 that leave the steam of expansion chamber;
-one comprises ring, the first area 512 of the caulking piece of plate or other form;
The loop 513 of-one liquid that leaves the tower bottom of being used to circulate, it comprises a pump 514; Grasshopper in jar 510 can be delivered in the jar 500 it to remove too much salts solution by pipeline 515;
-one second area 516, it comprises caulking piece or a series of bubble cap plate or equality unit;
The inlet 517 of-one water purification and/or the processing condensation product handled in advance;
The droplet separation device 518 of-one form such as textile mat, bubble plate or caulking piece;
Article-one, discharge of steam pipeline 519.
As a kind of modification, tower T can be replaced by a series of upright only members, and these members are stacked mutually, finish identical functions with multistage tower T.Equally, the neutralization zone 512 that comprises caulking piece can be replaced by Venturi reactor or equality unit.
The reagent conveying loop comprises:
The nitric acid loop of-proper concn comprises two pipelines 521,522, and pipeline 521 is used to supply reactor R, and pipeline 522 feeds the ammonium nitrate solution circulation loop 513 relevant with treating column; This pipeline 522 as a kind of modification, can directly feed treating column T;
Article-one, ammonia conveying loop, it also comprises two pipelines 523,524, supplies the upstream portion R of reactor respectively
1With middle portion R
2As a kind of modification, main ammonia line of pipes 523 can be distributed between two pipes, and a pipe feeds the upstream that the pipeline 524 that attached ammonia residual is provided enters the point of reactor, and another pipe then feeds the downstream of above-mentioned point.
As everybody knows, nitric acid and ammonia can preheatings in suitable heat exchanger (not shown), and the steam that heat exchanger preferably produces in the use equipment is so that improve the thermo-efficiency of reaction.
Equipment also is provided with control device 531,532,533,534, and its control is as the function of the set(ting)value of some parameters and observed value, the flow rate in each pipeline of equipment.
Above-mentioned control device acts on the valve that is separately positioned on each pipeline, the valve 541-545 that has only drawn main among the figure.
Control device will not made general detailed description, and the major function of finishing only is described, the device of implementing this control is that those skilled in the art is known.
Operation according to reactor of the present invention and equipment is as follows:
Neutralization reaction mostly takes place in reactor R.At part R
1In the acid and the flow rate of ammonia remain on the ratio that approaches stoichiometric ratio as far as possible through control, for example in ± 1%, preferably ammonia is excessive slightly.80% to 99% of total reaction agent stream, best 92% to 99%, the 98% upstream reaction chamber R that is introduced into reactor for example
1The concentration of nitric acid is 50% to 70%, is preferably 55% to 63%.When using sulfuric acid and phosphoric acid, concentration can be selected in 70% to 99% and 52% to 70% respectively.Ammonia is anhydrous gaseous form.
The ammonia of residue percentage ratio is admitted to second section R
2
In the example of Fig. 1, the ammonia of additional content is introduced into the middle portion R of reactor
2, its effect is to improve the output of reactor, the corrosion of restriction middle portion.In addition, constitute being subjected at utmost the pipe 121,122,123 of corrosive part easily and can thinking consumable product of reactor, its cost is significantly less than the cost of whole reactor.
In the embodiment of Fig. 2, at reactor middle portion R
2In be provided with interior pipe, the ammonia of additional content is introduced vacuum doughunt 227, this has just significantly limited the corrosion of the internals 221,222,223 of middle portion.
In the embodiment of Fig. 3 and 4, in first kind of situation, be provided with hole 328, in second kind of situation, be provided with contraction section 422 and 440, this just makes by managing 324,424 ammonia that leave and is sucked on the direction of interior pipe.The working conditions that depends on reactor in vacuum doughunt 327,427, can form a stream at downstream direction or reverse direction.In these two examples, this circulation can guarantee that nitrate is not detained at region intermediate, and in view of the explosivity of product, delay may cause danger.
As a kind of modification, the middle portion 121 that length is little; 221; 321; 421; 440 general available titaniums are made.
According to the present invention, the flow rate of the ammonia in the pipeline 524 is controlled so that at part R
2And R
3In obtain the excess ammonia that needs, and for example in expansion drum 500, obtain steam greater than 9 alkaline pH value.Therefore, device 532 controls are as the aperture of the valve 544 of the pH value function of measuring on the pipeline 501.
Nitrate solution separates in jar 500 in known manner with steam, and solution is collected in the bottom of jar, and steam is then discharged from top.
Pressure in this jar preferably remains on 1 to 8 crust, and in order can fully to expand in jar, the pressure downhill reaction device that is preferably in 5 to 10 crust is partly supplied ammonia and nitric acid.
The basic steam that enters treating column T neutralizes owing to adding washings, washings is that the mixture by the ammonium nitrate solution of recirculation at the bottom of tower and nitric acid constitutes, and regulates according to the pH value that is recycled to the ammonium nitrate solution of tower by the amount that pipeline 522 sprays into loop 513 or sprays into the nitric acid of tower T.The setting point of pH meter 533 is fixed to obtain acid enough washingss remaining ammonia that neutralizes.Above-mentioned pH meter acts on the by-pass valve control 542 of nitric acid pipeline 522.The concentration of acidic cleaning liquid is preferably between 5% and 20%, but also can increase to 40%.
The effect that above-mentioned tower is set is to neutralize fully, thereby obtains the steam of no ammonia, thereby two problems mentioning when presents begins all are resolved really.
Claims (19)
1. reactor of making ammonium salt, this reactor comprises a tubular reaction chamber (110; 210; 310; 410), at least one ammonia transfer lime (111; 211; 311; 411) and at least one sour transfer lime (112; 212; 312; 412), they are arranged in the first upstream portion (R of reactor
1) in, it is characterized in that: it also is included in a second section of arranging in the extension of first part, and it comprises a contraction section (122 on flow direction; 222; 322; 422), round shape part (121; 221; 321; 421) and an expansion (123; 223; 323; 423), be provided with at least one second ammonia transfer lime (124; 224; 324; 424), it feeds described reactor near the upstream extremity of described second section.
2. reactor as claimed in claim 1, it is characterized in that: described reactor second section comprises a unique pipe (121), its diameter is less than the diameter of the pipe that limits described reaction chamber (110), part is being extended a contraction section (122) at its upstream, is extending an expansion (123) in its downstream part.
3. reactor as claimed in claim 1, it is characterized in that: described reactor second section comprises pipe in an outer tube and, diameter of inner pipe is less than the diameter of the pipe that limits described reaction chamber, and part comprises a contraction section (222) at its upstream, comprise an expansion (223) in its downstream part, at outer tube (220) and interior pipe (221,222,223) form a ringwise substantially chamber (227) between, the internal capacity of interior pipe and vacuum doughunt are interconnected in its downstream end at least.
4. reactor as claimed in claim 3 is characterized in that: in the part, interior pipe (321) comprises a series of holes (328) at its upstream, and ammonia transfer lime (324) feeds outer tube (320) near described a series of holes (328).
5. reactor as claimed in claim 1, it is characterized in that: described reactor second section comprises an outer tube (420), on flow direction, in described outer tube, one first contraction section (440) is the interior pipe (421) of a diameter less than the diameter of the pipe that limits described reaction chamber (410) afterwards, interior pipe upstream extremity is extending a contraction section (422), its inlet diameter is greater than the exit diameter of first contraction section (440), in interior pipe downstream end an expansion (423) is arranged, the second ammonia transfer lime (424) feeds near the import of the contraction section (422) of interior pipe.
6. reactor as claimed in claim 5 is characterized in that: interior pipe (421,422,423) is fixed on outer tube (420) and is constituted reactor third part (R by a flange (426) near its downstream end
3) pipe (430) between.
7. reactor as claimed in claim 3 is characterized in that: interior pipe is provided with separator (329,429), and it is used for respect to outer tube is interior pipe guiding.
8. reactor as claimed in claim 3 is characterized in that: pipe comprises along its round shape part in described, at the strengthening rib (421a) of its contraction section and expansion extension.
9. reactor as claimed in claim 5 is characterized in that: near its downstream end, interior pipe (423) comprises a plurality of openings (428) that interior pipe internal capacity are connected in ringwise substantially chamber (427).
10. method of making ammonium salt, this method is included near the reagent that comprises at least a acid and ammonia of introducing in upstream of a tubular reactor (R), in expansion chamber (D), make salt and the vapor removal that leaves reactor in the solution then, it is characterized in that: 80% to 99% of total reaction agent stream is introduced in the upstream portion of reactor with stoichiometric ratio substantially, the upstream extremity of the reactor second section of the ammonia of rest part in the extension that is arranged in first part is introduced reactor, thereby make in expansion chamber isolated steam have the pH value of an alkalescence, contact with the remainder of acid by the alkaline steam that will leave expansion chamber neutralization reaction is finished in an additional step.
11. method as claimed in claim 10 is characterized in that: the amounts of reactants of introducing in the reactor upstream portion accounts for 92% to 99% of total reaction agent stream.
12. method as claimed in claim 10 is characterized in that: the ammonia stream of introducing in the reactor second section is controlled so that partly obtain the excess ammonia of needs in reactor downstream, and makes the steam of acquisition have alkaline pH value after expansion chamber separates.
13. method as claimed in claim 12 is characterized in that: the ammonia stream of introducing in the reactor second section is controlled so that partly obtain the excess ammonia of needs in reactor downstream, and makes the steam of acquisition have pH value greater than 9 after expansion chamber separates.
14. method as claimed in claim 10 is characterized in that: the described additional step that neutralization reaction is finished is to be undertaken by the washing soln that the mixture that uses by the ammonium salt of recirculation and acid the forms alkaline steam that neutralizes.
15. method as claimed in claim 10 is characterized in that: the acid amount of using in additional neutralization stage is as the function of the pH value of the ammonium salt solution of recirculation and be controlled.
16. be used for implementing the equipment as the manufacturing ammonium salt of each described method of claim 10 to 15, it comprises a tubular reactor, at least one ammonia transfer lime (111; 211; 311; 411) and at least one to feed reactor first part be the sour transfer lime (112 of upstream portion; 212; 312; 412), this reactor passes to an expansion chamber (D), in expansion chamber, salt in the solution and vapor removal, it is characterized in that: described reactor (R) is that each limits in the claim 1 to 9, described equipment also has an additional class (T), in additional class (T), the steam from expansion chamber (D) is contacted to realize neutralization completely with the remainder of acid.
17. equipment as claimed in claim 16, it is characterized in that: described additional neutralization level (T) comprises a treating column, treating column comprises a flow container (510), a device (511) that is used for spraying from the steam of expansion chamber (D), at least one sour jet apparatus (513,522), at least one is used to make steam and the sour zone (512) that contacts, a washing device (516,517) and be used to discharge the device (519) of no ammonia steam.
18., it is characterized in that: be provided with a loop (513,514) that is used for the salts solution of the additional neutralization level of recirculation production as claim 16 or 17 described equipment.
19. as claim 16 or 17 described equipment, it is characterized in that: expansion chamber (D) is sent in the overflow of the salts solution of producing in additional neutralization level (T).
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| FR9614028A FR2755959B1 (en) | 1996-11-18 | 1996-11-18 | REACTOR, PROCESS AND PLANT FOR THE MANUFACTURE OF AMMONIA SALTS |
| FR9614028 | 1996-11-18 |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1182636A CN1182636A (en) | 1998-05-27 |
| CN1075396C true CN1075396C (en) | 2001-11-28 |
Family
ID=9497716
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN97102296A Expired - Fee Related CN1075396C (en) | 1996-11-18 | 1997-01-20 | Reactor, process and plant for manufacturing ammonium salts |
Country Status (13)
| Country | Link |
|---|---|
| US (2) | US5904906A (en) |
| EP (1) | EP0842896A1 (en) |
| CN (1) | CN1075396C (en) |
| AU (1) | AU696790B2 (en) |
| CA (1) | CA2221038C (en) |
| FR (1) | FR2755959B1 (en) |
| HR (1) | HRP970623A2 (en) |
| NO (1) | NO317707B1 (en) |
| RU (1) | RU2146557C1 (en) |
| TR (1) | TR199701384A2 (en) |
| UA (1) | UA42832C2 (en) |
| YU (1) | YU49280B (en) |
| ZA (1) | ZA9772B (en) |
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| US7128880B2 (en) * | 2002-12-19 | 2006-10-31 | Environmental Technologies Capital Partners Llc | Organic recycling with a pipe-cross or tubular reactor |
| US20050288516A1 (en) * | 2004-06-28 | 2005-12-29 | Warren Jack S | Use of a device or devices, such as a convergent divergent funnel mixer, to optimize the available reaction volume, the raw material feed ratios and the weight hourly space velocity in a tube reactor |
| US7204968B2 (en) * | 2004-08-30 | 2007-04-17 | Reints John V | Method of producing heat energy |
| US8105413B2 (en) | 2005-02-23 | 2012-01-31 | Vitag Corporation | Manufacturing of bioorganic-augmented high nitrogen-containing inorganic fertilizer |
| CN101132988B (en) * | 2005-03-02 | 2012-06-27 | 亚拉国际有限公司 | Tubular reactor and device especially used for preparing urea ammonium sulfate |
| US8192519B2 (en) | 2005-03-09 | 2012-06-05 | Vitag Corporation | Beneficiated, heat-dried biosolid pellets |
| CA2622881C (en) | 2005-09-15 | 2015-01-27 | Vitag Llc | Organic containing sludge to fertilizer alkaline conversion process |
| US9695092B2 (en) | 2006-02-23 | 2017-07-04 | Anuvia Plant Nutrients Corporation | Process for treating sludge and manufacturing bioorganically-augmented high nitrogen-containing inorganic fertilizer |
| WO2008101250A1 (en) | 2007-02-16 | 2008-08-21 | Vitag Corporation | Process for treating sludge and manufacturing bioorganically-augmented high nitrogen-containing inorganic fertilizer |
| JP2012516935A (en) * | 2009-02-05 | 2012-07-26 | ダウ グローバル テクノロジーズ エルエルシー | Low density polyethylene (LDPE) tubular reactor for injecting peroxide initiator |
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| AR084076A1 (en) | 2010-12-01 | 2013-04-17 | Orica Int Pte Ltd | PROCESS TO PRODUCE NITRIC ACID |
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| US8974763B1 (en) | 2013-12-18 | 2015-03-10 | Rentech, Inc. | System and method for production of granular ammonium sulfate |
| EP3302782A4 (en) | 2015-06-05 | 2019-01-09 | Anuvia Plant Nutrients Holdings, LLC | High value organic containing fertilizers and methods of manufacture |
| FR3039830B1 (en) * | 2015-08-03 | 2018-09-07 | Ocp Sa | PROCESS FOR PRODUCING AN AMMONIUM PHOSPHATE FERTILIZER WITH A REDUCED CADMIUM CONTENT |
| RU2619700C9 (en) * | 2016-04-05 | 2017-07-24 | федеральное государственное бюджетное образовательное учреждение высшего образования "Казанский национальный исследовательский технологический университет" (ФГБОУ ВО "КНИТУ") | Method for ammonium nitrate preparation, and device for its implementation |
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| EP3909673A1 (en) * | 2020-05-12 | 2021-11-17 | Casale Sa | Process for making ammonium nitrate |
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| US2902342A (en) * | 1955-01-27 | 1959-09-01 | Jr Bernard J Kerley | Method and apparatus for producing ammonium salts |
| CN87107538A (en) * | 1986-12-18 | 1988-07-20 | 氮及肥田料化学公司 | new tubular reactor |
| EP0277901A1 (en) * | 1987-01-21 | 1988-08-10 | Union Explosivos Rio Tinto, S.A. | Process and installation for the production of ammonium nitrate |
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| NL7805957A (en) * | 1978-06-01 | 1979-12-04 | Unie Van Kunstmestfab Bv | PROCESS AND EQUIPMENT FOR THE PREPARATION OF A PRODUCT CONTAINING AMMONIUM ORTHOPHOSPHATE AND ANY PRODUCT OBTAINED BY THIS PROCESS. |
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- 1996-11-18 FR FR9614028A patent/FR2755959B1/en not_active Expired - Fee Related
-
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- 1997-01-06 ZA ZA9772A patent/ZA9772B/en unknown
- 1997-01-20 CN CN97102296A patent/CN1075396C/en not_active Expired - Fee Related
- 1997-03-17 AU AU16287/97A patent/AU696790B2/en not_active Ceased
- 1997-11-10 CA CA002221038A patent/CA2221038C/en not_active Expired - Fee Related
- 1997-11-12 EP EP97402700A patent/EP0842896A1/en not_active Withdrawn
- 1997-11-14 US US08/970,208 patent/US5904906A/en not_active Expired - Lifetime
- 1997-11-14 NO NO19975232A patent/NO317707B1/en unknown
- 1997-11-17 HR HR970623A patent/HRP970623A2/hr not_active Application Discontinuation
- 1997-11-17 RU RU97119730A patent/RU2146557C1/en not_active IP Right Cessation
- 1997-11-17 UA UA97115501A patent/UA42832C2/en unknown
- 1997-11-18 TR TR97/01384A patent/TR199701384A2/en unknown
- 1997-11-18 YU YU45197A patent/YU49280B/en unknown
-
1999
- 1999-02-12 US US09/249,549 patent/US6117406A/en not_active Expired - Lifetime
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| US2902342A (en) * | 1955-01-27 | 1959-09-01 | Jr Bernard J Kerley | Method and apparatus for producing ammonium salts |
| CN87107538A (en) * | 1986-12-18 | 1988-07-20 | 氮及肥田料化学公司 | new tubular reactor |
| CN1013490B (en) * | 1986-12-18 | 1991-08-14 | 氮及肥田料化学公司 | Improved pipe reactor for the mfr. of ammonium phosphates containing ammonium sulfate |
| EP0277901A1 (en) * | 1987-01-21 | 1988-08-10 | Union Explosivos Rio Tinto, S.A. | Process and installation for the production of ammonium nitrate |
Also Published As
| Publication number | Publication date |
|---|---|
| ZA9772B (en) | 1998-07-06 |
| YU49280B (en) | 2005-03-15 |
| US6117406A (en) | 2000-09-12 |
| YU45197A (en) | 1999-09-27 |
| NO975232D0 (en) | 1997-11-14 |
| UA42832C2 (en) | 2001-11-15 |
| RU2146557C1 (en) | 2000-03-20 |
| FR2755959B1 (en) | 1998-12-24 |
| CA2221038A1 (en) | 1998-05-18 |
| AU696790B2 (en) | 1998-09-17 |
| EP0842896A1 (en) | 1998-05-20 |
| CN1182636A (en) | 1998-05-27 |
| NO975232L (en) | 1998-05-19 |
| HRP970623A2 (en) | 2000-06-30 |
| US5904906A (en) | 1999-05-18 |
| FR2755959A1 (en) | 1998-05-22 |
| TR199701384A2 (en) | 1998-06-22 |
| NO317707B1 (en) | 2004-12-06 |
| AU1628797A (en) | 1998-06-11 |
| CA2221038C (en) | 2000-04-18 |
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